EP3218308B1 - Procédé de réduction de chrome hexavalent dans des matières solides oxydées - Google Patents

Procédé de réduction de chrome hexavalent dans des matières solides oxydées Download PDF

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Publication number
EP3218308B1
EP3218308B1 EP15784937.3A EP15784937A EP3218308B1 EP 3218308 B1 EP3218308 B1 EP 3218308B1 EP 15784937 A EP15784937 A EP 15784937A EP 3218308 B1 EP3218308 B1 EP 3218308B1
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weight
process according
volume
atmosphere
reactor
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EP3218308A1 (fr
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Rainer Ortmann
Holger Friedrich
Matthias Boll
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Lanxess Deutschland GmbH
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Lanxess Deutschland GmbH
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Priority to PL15784937T priority Critical patent/PL3218308T3/pl
Priority to SI201530395T priority patent/SI3218308T1/sl
Priority to HRP20181435TT priority patent/HRP20181435T1/hr
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G49/00—Compounds of iron
    • C01G49/0018—Mixed oxides or hydroxides
    • C01G49/0045—Mixed oxides or hydroxides containing aluminium
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G37/00—Compounds of chromium
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B34/00—Obtaining refractory metals
    • C22B34/30—Obtaining chromium, molybdenum or tungsten
    • C22B34/32—Obtaining chromium

Definitions

  • the invention relates to a process for the reduction of hexavalent chromium, Cr (VI), in oxidic solids.
  • Cr hexavalent chromium
  • Cr chrome ore residues
  • COPR Chromite Ore Processing Residue
  • chromium spinels especially the chromite (chromium ironstone, idealized: FeCr 2 O 4 ), are of economic importance.
  • chromite and sodium alkalis especially sodium carbonate
  • substances are added to the kiln mixture that are supposed to preserve the porosity of the kiln contents during digestion (so-called leaning agents).
  • the porosity is required to provide sufficient surface area for reaction with oxygen.
  • the chromium yield when using chromite is in the range of 74% to 90% of chromium present in chrome ore.
  • the separation of the dissolved monochromate is carried out after cooling and leaching at a set by the addition of acids or dichromate pH by means of solid-liquid separation, usually via filtration.
  • the insoluble residue is leached several times to reduce the content of water-soluble Cr (VI).
  • a portion of the residue may be dried to be recycled to the oven mixture as a leaning agent.
  • Part of the Cr (VI) is still present in water-soluble form as sodium monochromate, but leaching at low Cr (VI) levels makes economic sense no longer.
  • part of the Cr (VI) is also present in a water-insoluble or water-sparingly soluble form, which likewise can not be recovered with economically justifiable expense.
  • the chrome ore residue may vary in composition, in particular in the CaO content.
  • Chromium ore residues from the high lime process have up to 35 wt .-% CaO, those from the no lime process usually less than 5 wt .-%, while those from the low lime process from 5 to 35 wt. % lie.
  • the chromium ore residue has therefore been subjected to a reduction process for several decades, usually in order to convert the remaining Cr (VI) into harmless Cr (III), before finally depositing it. It is important that as complete as possible reduction of the existing Cr (VI) is achieved, including the non-located on the surface of the residue, but of a silica and / or alumina layer trapped, difficult to access and water-insoluble or wasserthrolösliche Cr (VI) is included.
  • the US 2010/0135876 A1 discloses a wet chemical process for the reduction of Cr (VI) in chrome ore residues, in which Fe (II) ions, which act as reducing agents, are "fixed" on the surface of the COPR particles in the form of a sparingly soluble precipitate and thus also capable should be effective over a longer period of time.
  • Fe (II) ions which act as reducing agents, are "fixed" on the surface of the COPR particles in the form of a sparingly soluble precipitate and thus also capable should be effective over a longer period of time.
  • the Cr (VI) contained in the COPR matrix is dissolved by adding a sufficient amount of Fe (II) sulfate.
  • the Fe (II) ions also reduce the liberated Cr (VI) to Cr (III).
  • Fe (OH) 3 and Al (OH) 3 as well as CaSO 4 precipitate, favoring the dissolution of the COPR particles.
  • Excess Fe (II) is then "fixed" in the form of a sparingly soluble precipitate on the surface of the COPR particles. This is preferably done by adding a sulfide, for example, sodium sulfide (Na 2 S), sodium hydrosulfide (NaHS) or calcium polysulfide (CaS x ), whereby iron (II) sulfides are precipitated or by addition of phosphoric acid, whereby Fe (II) phosphates precipitated become.
  • a sulfide for example, sodium sulfide (Na 2 S), sodium hydrosulfide (NaHS) or calcium polysulfide (CaS x ), whereby iron (II) sulfides are precipitated or by addition of phosphoric acid, whereby Fe (II) phosphates precipitated become.
  • FeS is known to degrade in boiling water. Under the conditions of the alkaline digestion process according to USEPA SW-846 Method 3060A Fe
  • US 2010/0135876 A1 the phenomenon that after drying the COPR samples reduced only with Fe (II) sulfate with the aid of the alkaline digestion process again significant amounts of Cr (VI) (about 1100 ppm or 1500 ppm) can be detected. They attribute this either to a reoxidation of Cr (III) to Cr (VI) with atmospheric oxygen or to the oxidation of Fe (II) to Fe (III) with atmospheric oxygen.
  • the US 2010/0135876 A1 does not consider that the resolution of Cr (VI) bound in the COPR matrix is incomplete.
  • nanoparticulate iron particles sino-called zero valent iron
  • a disadvantage of this method is that the nanoparticulate iron particles ( ⁇ 100 nm, specific surface area about 35 m 2 / g) are very expensive to produce and therefore at most suitable for laboratory experiments, but not currently for an application on an industrial scale in question come.
  • the nanoparticle iron particles are slowly oxidized by air and / or moisture, so that it is doubtful that this material will be able to reduce chromium chromium in hexavalent chromium over years.
  • reaction time There was a systematic variation of the reaction time, reaction temperature and the amount of reducing agent added. It shows that at 600 ° C reaction temperature, a mass ratio of 2.0: 1 (reducing agent: Cr (VI)) is required to obtain a complete reduction at 20 min reaction time.
  • Zhang et al. also describe the reduction of Cr (VI) contained in chrome ore residue with sewage sludge via pyrolysis.
  • the sludge is mixed in a ratio of 1:10 with chromium ore residue and then subjected to pyrolysis at 600 ° C.
  • Digestion of the Cr (VI) is also carried out according to the alkaline digestion procedure described in USEPA SW-846 Method 3060A. Also in this process, the Cr (VI) content can be reduced from the original 3384 ppm for the untreated chrome ore residue to only 24 ppm.
  • the US 2004/0086438 A1 discloses a method by which the chromium and iron present in chromium ore residue can be simultaneously recovered.
  • the chromium ore residue is first treated with at least 20% by weight of a metal hydroxide, preferably sodium or potassium or lithium hydroxide, at at least 350 ° C. for at least 10 minutes in air. This is followed by an acidic workup, which leads to an iron-rich insoluble residue.
  • a metal hydroxide preferably sodium or potassium or lithium hydroxide
  • WO2014 / 006196 discloses a process for the reduction of hexavalent chromium in oxidic solids, in which the oxidic solid is mixed with a carbonaceous compound which is liquid in the range from 20 to 100 ° C, such as glycerol or polyethylene glycol, which serves as a reducing agent.
  • a Cr (VI) content of ⁇ 1000 ppm can be detected, preferably less than 100 ppm.
  • the disadvantages caused by the use of the reducing agents of the prior art, such as required exhaust air treatment, problematic metering of the reducing agent and increased costs should be overcome.
  • Chromium (VI) compounds are considered to be of very high concern according to the REACH Regulation and are listed on the SVHC (Substances Of Very High Concern) list. Product mixtures containing more than or equal to 1000 ppm chromium (VI) must therefore be labeled accordingly (Regulation 1272/208 / EC and 1999/45 / EC).
  • reducing agent is understood as meaning at least one compound which reduces Cr (III) to Cr (III) at least under the reaction conditions Cr (VI) prevailing in steps a) and b).
  • no reducing agent added means that no reducing agent is added to the oxidic solid and to the atmosphere containing less than 0.1% by volume of an oxidizing gas. Most preferably, no reducing agent is added to the entire process according to the invention.
  • One of the benefits of the process according to the invention is that the resulting reduced oxidic solid, in particular the reduced chromium ore residue, no longer has to be regarded and disposed of as a hazardous substance, but can be incorporated into a new value-added chain as valuable material.
  • the non-addition of a reducing agent in the process according to the invention affords numerous advantages over the reduction processes of the prior art: on the one hand, there is a clear cost advantage since reducing agent costs are eliminated. Furthermore, the implementation is technically significantly simplified by the elimination of metering of the reducing agent and by the omission of the use of a mixer which mixes the oxidic solid and the reducing agent. Furthermore, the exhaust gas treatment is significantly simplified, since the exhaust no longer contains any residues to be treated of organic or inorganic decomposition products of the reducing agent.
  • chromium ore residues which are obtained during the oxidative alkaline decomposition of chromium ore, for example chromite for the preparation of sodium monochromate.
  • a chromium ore residue which, in the production process of sodium monochromate proceeding from chromite, is obtained via an oxidative alkaline digestion with sodium carbonate (no-lime process, CaO content of ⁇ 5% by weight).
  • residues containing Cr (VI) such as those obtained, for example, from the preparation and further processing of sodium monochromate
  • the other residue containing Cr (VI), particularly preferably calcium vanadate, being used in the removal of vanadium from the Monochromate solution is formed is used.
  • mixtures of oxidic solids Preferably, such a mixture contains chromium ore residues and other residues, containing Cr (VI), as obtained, for example, from the preparation and further processing of sodium monochromate, wherein as the other residue, containing Cr (VI), especially preferably calcium vanadate, which is formed in the separation of vanadium from the monochromate solution, is used.
  • the oxidic solids can be further metal oxides such as chromium (III) oxide (Cr 2 O 3 ), aluminum oxide (Al 2 O 3 ), iron (III) oxide (Fe 2 O 3 ), magnesium oxide (MgO), calcium oxide (CaO), Silica (SiO 2 ), vanadium oxide (V 2 O 5 ), sodium oxide (Na 2 O), and sodium monochromate (Na 2 CrO 4 ).
  • the oxidic solids preferably contain a Cr (VI) content of up to 80,000 ppm, particularly preferably up to 50,000 ppm, most preferably from 1,000 to 15,000 ppm, determined according to the modified alkaline digestion method based on USEPA SW-846 Method 3060A ,
  • the Cr (VI) is preferably present in the oxidic solids as sodium monochromate (Na 2 CrO 4 ).
  • the oxidic solids can be supplied as water-containing filter cake to step a). In a preferred embodiment of the process according to the invention, however, they are used in dried form. Particularly preferably, they have a moisture content of max. 2.0 wt .-%, most preferably less than 1.0 wt .-%, on.
  • the CaO content of the oxidic solid is preferably less than 15 wt .-%, most preferably less than 10 wt .-%, in particular less than 5 wt .-%.
  • the chrome ore residues usually accumulate in the production process of sodium monochromate after solid-liquid separation as moist filter cake, which can thus be fed to step a).
  • Other residues, containing Cr (VI) are preferably used with a vanadium content of 12 to 15 wt .-%.
  • Mixtures of chrome ore residue and vanadate-containing other residue preferably contain up to 15,000 ppm of Cr (VI).
  • Mixtures of oxidic solids preferably contain at least 85% by weight of chrome ore residues, more preferably at least 90% by weight of chrome ore residues.
  • Oxidic solids are preferably used for the process according to the invention, in which at least 90% of the particles are smaller than 500 ⁇ m, very particularly preferably smaller than 300 ⁇ m. This can - if necessary - be achieved by a step a) upstream screening and / or grinding.
  • the atmosphere in step a) contains less than 0.1% by volume of an oxidizing gas, the oxidizing gas preferably being oxygen.
  • the atmosphere in step a) preferably contains less than 0.01% by volume of an oxidizing gas.
  • the atmosphere in step a) containing less than 0.1 vol .-%, preferably less than 0.01 vol .-%, of an oxidizing gas selected from the group consisting of inert gas atmosphere and vacuum.
  • the atmosphere in step a) containing less than 0.1 vol .-%, more preferably less than 0.01 vol .-%, of an oxidizing gas, inert gas atmosphere.
  • the inert gas atmosphere preferably consists of at least 90% by volume, preferably at least 95% by volume, very particularly preferably at least 99% by volume, very particularly preferably at least 99.5% by volume selected from one or more gases the group consisting of noble gases, in particular of helium and argon, nitrogen and carbon dioxide, preferably selected from the group consisting of nitrogen and carbon dioxide, very particularly preferably nitrogen.
  • the inert gas is passed over the oxidic solid, more preferably by means of an inert gas, most preferably by means of an inert gas of about one third of the reactor volume / min, most preferably by means of an inert gas of about one third of the reactor volume / min at atmospheric pressure in the reactor (about 1013 mbar).
  • the atmosphere in step a) containing less than 0.1 vol .-%, more preferably less than 0.01 vol .-%, of an oxidizing gas, vacuum.
  • vacuum is preferably understood as meaning an atmosphere having a pressure of less than 800 mbar, particularly preferably less than 650 mbar, very particularly preferably less than 450 mbar.
  • the oxidic solid is heated in step a) to a temperature of 600 ° C to 1400 ° C, preferably to a temperature of 850 ° C to 1200 ° C, most preferably to a temperature of 950 ° C to 1150 ° C.
  • the reaction time depends on the temperature used and can be easily determined in a manner well known to those skilled in the art.
  • the reaction time is preferably from five minutes to 24 hours, preferably from 1 to 10 hours.
  • the heating in step a) is preferably carried out in a reactor.
  • Suitable reactors are all devices which can ensure the temperatures required in step a) and the atmosphere required in step a) containing less than 0.1% by volume of an oxidizing gas.
  • the heating in step a) can be carried out in a continuous or discontinuous reactor.
  • the heating in step a) preferably takes place in a continuously operating reactor.
  • the reactor can be indirectly or directly heated, wherein preferably an indirectly heated reactor is used in step a). Particular preference is given to using in step a) a gas-heated or electrically indirectly heated reactor, very particularly preferably an electrically indirectly heated reactor.
  • indirectly heated reactors also has the advantage that in the reaction space itself only a very small gas flow prevails, whereby hardly any dust is discharged.
  • furnaces in step a for example furnaces of various types can be used.
  • the person skilled in common ovens such as oven rack, muffle furnace, tube furnace, convection oven and retort oven are known.
  • the furnace used in step a) is a tubular furnace, more preferably a horizontal tubular furnace, most preferably a two-zone rotary kiln.
  • the oxidic solid may be present in step a) in any manner which is inert to the reaction conditions prevailing in step a).
  • the oxidic solid is preferably present in a crucible during heating, particularly preferably in a silicon carbide crucible.
  • step b) the cooling of the reaction product obtained according to step a) in an atmosphere containing less than 0.1 vol .-% of an oxidizing gas to a temperature of less than 100 ° C.
  • the cooling in step b) is preferably carried out in a reactor.
  • Suitable reactors are all devices which can ensure the temperatures required in step b) and the atmosphere required in step b) containing less than 0.1% by volume of an oxidizing gas.
  • step b) The preferred ranges for the atmosphere containing less than 0.1% by volume of an oxidizing gas listed under step a) and for the reactors listed under step a) corresponding to step b) apply.
  • step b) The reaction product obtained after step a) is preferably cooled in step b) to a temperature below 40 ° C., particularly preferably below 30 ° C.
  • a reoxidation of Cr (III) to Cr (VI) can be effectively avoided, as studies have shown.
  • step a) The cooling of the reaction product obtained according to step a) can be carried out in step b) such that the reaction product obtained after step a) remains in the reactor and the reactor is cooled by switching off the indirect heating by means of inert gas.
  • the cooling of the reaction product obtained after step a) can also be carried out in step b) such that the reaction product obtained after step a) remains in the reactor and is cooled in vacuo.
  • the cooling of the reaction product obtained in step a) in step b) can also be carried out in a continuously operating or discontinuously operating cooling unit, wherein it is preferably carried out in a continuously operating cooling unit.
  • continuously operating refrigeration units only fixed bed heat exchangers, screw heat exchangers (cooling screws) or cooling drums are mentioned here.
  • step a) and b) The use of a rotary kiln with two temperature zones is also conceivable for the combined use in step a) and b).
  • the cooling of the reaction product obtained in step a) in step b) can consequently also be carried out in a two-zone rotary kiln.
  • step b) If a discontinuously operating reactor was used in step a), the cooling in step b) can also take place in the reactor itself, which is technically particularly easy to implement.
  • reaction product obtained from step a) it is also possible to quench the reaction product obtained from step a) under a protective gas atmosphere in water. This allows a quick and easy cooling.
  • the reaction product is obtained as an aqueous suspension, which must be further worked up, for example via a solid / liquid separation and subsequent drying. This makes little sense from an energetic point of view, because the reaction product obtained from step a) is already dry and can be further processed directly. That after The cooled reaction product obtained in step b) may optionally be subjected to sieving and / or grinding.
  • the Cr (VI) content of the cooled reaction product obtained after step b) is determined according to the disclosed modified alkaline digestion process.
  • a reduced oxidic solid is obtained.
  • a reduced oxidic solid is obtained, which is characterized in that it contains less than 15% by weight of calcium oxide, more preferably less than 10% by weight of calcium oxide, most preferably less than 5% by weight of calcium oxide ,
  • the reduced oxidic solid contains less than 1000 ppm Cr (VI), more preferably less than 100 ppm Cr (VI), most preferably less than 50 ppm Cr (VI).
  • the oxidic solid contains more than 2 wt .-% water, it is dried to constant weight at 120 ° C and then weighed. In contrast to the method described in USEPA SW-846 Method 3060A, however, 2.4 g to 2.6 g of the sample to be analyzed are not digested, but between 9.9 g and 10.1 g (weighing accuracy 0.0001 g) of the oxidic solid are quantitatively introduced into a reaction flask with protective gas connection transferred.
  • the mother liquor and washings obtained in the filtration and washing are combined in a 500 ml volumetric flask, made up to the calibration mark with demineralized water and analyzed for Cr (VI) as described below.
  • a significantly larger amount of sample is used, but eventually the alkaline extract in the volumetric flask is made up to 500 ml instead of 250 ml.
  • the procedure described above results in twice as high Cr (VI) concentration in the standard solution used for Cr (VI) determination via UV / VIS spectroscopy, compared to the method described in USEPA SW-846 Method 3060A.
  • a small amount of the clear solution is taken from the volumetric flask obtained with the alkaline extract from the alkaline digestion method and adjusted to a pH of 7 with dilute hydrochloric acid. This usually produces a precipitate of aluminum and silicon hydroxides, which is centrifuged off. The resulting clear centrifugate is still through a Filtered 0.45 micron syringe filter and determined its Cr (VI) content after adjustment of the pH as a 1,5-diphenylcarbazide complex by means of UV / Vis spectroscopy, as described in USEPA Method 218.7. The measured Cr (VI) concentration, if it can be quantified, is calculated back to the mass of the oxidic solids quantity originally used, taking into account the dilution produced by the pH adjustment with the dilute hydrochloric acid.
  • the determination of the Cr (VI) content was carried out on an automated UV / Vis spectrometer of the Metrohm 844 UV / VIS Compact IC type at a wavelength of 539 nm.
  • the monochromate is first separated from other anions via an anion exchange column before it is reacted in a post-column reactor with 1,5-diphenylcarbazide and determined spectrophotometrically.
  • the Cr (VI) determination limit is 0.0128 mg / L Cr (VI).
  • chrome ore residue from the industrial production process of sodium monochromate starting from chromite was used via an oxidative alkaline digestion with sodium carbonate (so-called no-lime method, CaO content ⁇ 5% by weight).
  • no-lime method CaO content ⁇ 5% by weight.
  • the chrome ore residue produced in the production process of sodium monochromate after solid-liquid separation in the form of a moist filter cake was merely dried but not sieved or ground.
  • Dried chromium ore residue whose Cr (VI) content was determined by the modified alkaline digestion method described above, was heated in an electrically indirectly heated horizontal tubular profil in crucibles.
  • the pipe diameter was 70 mm with a total length of 1500 mm, of which about 500 mm were heated.
  • the crucibles were in the heated area during the experiments.
  • the dried chrome ore residue was placed in the cold oven, gas sealed on both sides and nitrogen introduced from one side (> 99.9990 vol .-% nitrogen), which was passed on the opposite side via an outlet and a dive into the exhaust air.
  • the black reduced chromium ore reaction product was removed and worked up according to the alkaline digestion procedure described above, and the Cr (VI) content in the alkaline extract was determined by UV / Vis spectroscopy.

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Claims (15)

  1. Procédé de réduction du chrome hexavalent dans des solides oxydiques, contenant les étapes suivantes :
    a) le chauffage du solide oxydique, contenant Cr(VI), dans une atmosphère contenant moins de 0,1 % en volume d'un gaz oxydant à une température de 600 à 1 400 °C, et
    b) le refroidissement du produit de réaction obtenu selon l'étape a) dans une atmosphère contenant moins de 0,1 % en volume d'un gaz oxydant à une température inférieure à 100 °C,
    caractérisé en ce qu'aucun réducteur n'est ajouté au solide oxydique et à l'atmosphère aux étapes a) et b) dans le procédé.
  2. Procédé selon la revendication 1, caractérisé en ce que le solide oxydique utilisé est un résidu de minerai de chrome.
  3. Procédé selon l'une quelconque des revendications 1 ou 2, caractérisé en ce que le solide oxydique utilisé comprend jusqu'à 80 000 ppm, de préférence jusqu'à 50 000 ppm, de manière particulièrement préférée 1 000 à 15 000 ppm de Cr(VI).
  4. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que le Cr(VI) dans le solide oxydique se présente sous la forme de monochromate de sodium (Na2CrO4).
  5. Procédé selon l'une quelconque des revendications 1 à 4, caractérisé en ce que le solide oxydique présente la composition suivante :
    - oxyde de chrome (III) (Cr2O3) : 7 à 13 % en poids, de préférence 7,5 à 12,5 % en poids,
    - oxyde d'aluminium (Al2O3) : 10 à 30 % en poids, de préférence 18 à 24 % en poids,
    - oxyde de fer (III) (Fe2O3) : 42 à 50 % en poids, de préférence 42 à 48 % en poids,
    - oxyde de magnésium (MgO) : 9 à 18 % en poids, de préférence 10 à 17 % en poids,
    - oxyde de calcium (CaO) : < 10 % en poids, de préférence < 5 % en poids,
    - oxyde de silicium (SiO2) : 0 à 3 % en poids, de préférence 1 à 3 % en poids,
    - oxyde de vanadium (V2O5) : < 1 % en poids, de préférence < 0,5 % en poids,
    - oxyde de sodium (Na2O) : 0 à 5 % en poids, de préférence 2 à 5 % en poids,
    - monochromate de sodium (Na2CrO4) : 0,3 à 4,7 % en poids.
  6. Procédé selon l'une quelconque des revendications 1 à 5, caractérisé en ce qu'au moins 90 % des particules du solide oxydique sont inférieures à 500 µm, de manière particulièrement préférée inférieures à 300 µm.
  7. Procédé selon l'une quelconque des revendications 1 à 6, caractérisé en ce que l'atmosphère à l'étape a) contenant moins de 0,1 % en volume, de préférence moins de 0,01 % en volume, d'un gaz oxydant est choisie dans le groupe constitué par une atmosphère de gaz inerte et un vide.
  8. Procédé selon la revendication 7, caractérisé en ce que l'atmosphère à l'étape a) contenant moins de 0,1 % en volume, de préférence moins de 0,01 % en volume, d'un gaz oxydant, est une atmosphère de gaz inerte, et est constituée par au moins 90 % en volume, de préférence au moins 95 % en volume, de manière particulièrement préférée au moins 99 % en volume, de manière tout particulièrement préférée au moins 99,9 % en volume, d'un ou de plusieurs gaz choisis dans le groupe constitué par les gaz nobles, notamment l'hélium et l'argon, l'azote et le dioxyde de carbone, de préférence choisis dans le groupe constitué par l'azote et le dioxyde de carbone, de manière tout particulièrement préférée l'azote.
  9. Procédé selon la revendication 7, caractérisé en ce que l'atmosphère à l'étape a) contenant moins de 0,1 % en volume, de préférence moins de 0,01 % en volume, d'un gaz oxydant, est un vide, de préférence une atmosphère ayant une pression inférieure à 800 mbar, de manière particulièrement préférée inférieure à 650 mbar, de manière tout particulièrement préférée inférieure à 450 mbar.
  10. Procédé selon l'une quelconque des revendications 1 à 9, caractérisé en ce que le solide oxydique à l'étape a) est porté à une température de 850 °C à 1 200 °C, de préférence à une température de 950 °C à 1 150 °C.
  11. Procédé selon l'une quelconque des revendications 1 à 10, caractérisé en ce que le chauffage à l'étape a) a lieu dans un réacteur fonctionnant de manière continue ou fonctionnant de manière discontinue, de préférence dans un réacteur fonctionnant de manière continue.
  12. Procédé selon la revendication 11, caractérisé en ce que le réacteur est un réacteur à chauffage indirect avec un gaz ou électrique, de préférence un réacteur à chauffage indirect électrique.
  13. Procédé selon l'une quelconque des revendications 11 ou 12, caractérisé en ce que le réacteur est un four tubulaire horizontal à chauffage indirect électrique, de préférence un four tubulaire rotatif à deux zones.
  14. Procédé selon l'une quelconque des revendications 1 à 13, caractérisé en ce que le produit de réaction obtenu selon l'étape a) est refroidi à l'étape b) à une température inférieure à 40 °C, de manière particulièrement préférée inférieure à 30 °C.
  15. Procédé selon l'une quelconque des revendications 1 à 14, caractérisé en ce que le produit de réaction obtenu selon l'étape a) reste dans le réacteur à l'étape b) et le réacteur est refroidi avec un gaz inerte après l'arrêt du chauffage indirect.
EP15784937.3A 2014-11-13 2015-10-14 Procédé de réduction de chrome hexavalent dans des matières solides oxydées Not-in-force EP3218308B1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
PL15784937T PL3218308T3 (pl) 2014-11-13 2015-10-14 Sposób redukcji sześciowartościowego chromu w tlenkowych substancjach stałych
SI201530395T SI3218308T1 (sl) 2014-11-13 2015-10-14 Postopek redukcije šest valentnega kroma v trdnih oksidnih snoveh
HRP20181435TT HRP20181435T1 (hr) 2014-11-13 2015-10-14 Postupak za smanjenje šesterovalentnog kroma u oksidnim krutinama

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EP14193035.4A EP3020690A1 (fr) 2014-11-13 2014-11-13 Procédé de réduction de chrome hexavalent dans des matières solides oxydées
PCT/EP2015/073770 WO2016074878A1 (fr) 2014-11-13 2015-10-14 Procédé de réduction de chrome hexavalent dans des matières solides oxydiques

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EP3218308B1 true EP3218308B1 (fr) 2018-06-13

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EP (2) EP3020690A1 (fr)
CN (1) CN107108259A (fr)
AR (1) AR102645A1 (fr)
DK (1) DK3218308T3 (fr)
ES (1) ES2685904T3 (fr)
HR (1) HRP20181435T1 (fr)
HU (1) HUE039006T2 (fr)
LT (1) LT3218308T (fr)
PL (1) PL3218308T3 (fr)
PT (1) PT3218308T (fr)
RU (1) RU2017120378A (fr)
SI (1) SI3218308T1 (fr)
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EP3628753B1 (fr) 2018-09-26 2022-05-04 Brother Group (Hong Kong) Limited Procédé pour préparer des pastilles contenant du fer et du chrome
EP3760748B1 (fr) 2019-07-02 2023-09-20 Brother Group (Hong Kong) Limited Procédé de préparation de pastilles calcinées optimisées contenant du fer et du chrome
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CN115874067B (zh) * 2023-01-04 2025-09-12 北京科技大学 一种从高铬型钒渣中分离钒铬的方法

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ES2685904T3 (es) 2018-10-15
LT3218308T (lt) 2018-10-10
PL3218308T3 (pl) 2018-11-30
RU2017120378A3 (fr) 2019-03-28
AR102645A1 (es) 2017-03-15
EP3020690A1 (fr) 2016-05-18
US20180282176A1 (en) 2018-10-04
WO2016074878A1 (fr) 2016-05-19
HRP20181435T1 (hr) 2018-10-19
RU2017120378A (ru) 2018-12-13
DK3218308T3 (en) 2018-10-01
HUE039006T2 (hu) 2018-12-28
SI3218308T1 (sl) 2018-10-30
CN107108259A (zh) 2017-08-29
PT3218308T (pt) 2018-10-15
EP3218308A1 (fr) 2017-09-20

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